• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    1. THE METHOD OF CONTINUOUS GASIFICATION OF CARBON-CONTAINING MATERIAL IN A REACTOR WITH MOLTEN by supplying carbon-containing material and oxygen; process by improving the energy balance, in addition to the gas supplied to the melt under its surface, an oxygen-containing gas jet is fed to the surface of the melt from a height at which ix distance between the outlet of means for feeding kisloroda.i melt surface to the diameter means for supplying oxygen is 50t200. 2. The method according to claim 1, about tl and tea, and also with the fact that technically “8 pure oxygen” is used as the gas stream supplied to the melt surface. (L 3. Method according to Claim 1, in connection with the fact that air is used as the gas jet supplied to the surface of the melt. 4. Method according to claim 1-3, characterized in that it is supplied to The surface of the acid-melt-containing melt is pre-heated by a gas jet. SP a: O)
    公开号:SU1148566A3
    申请号:SU813320744
    申请日:1981-08-17
    公开日:1985-03-30
    发明作者:Фон Богданды Людвиг；Бротцман Карл
    申请人:Клекнер-Верке Аг (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to a method for the gasification of carbon-containing materials, in particular to a method for the gasification of carbon-containing material in a molten iron reactor. A known method of continuous gasification of carbon-containing material in a molten iron reactor by supplying carbon-containing material and oxygen-containing gas under the melt surface and removing gases formed in the gas space above the melt surface. J. However, the known method is not sufficiently economical because the heat loss during the gasification process These are compensated for by increasing the energy consumption spent on the process, which negatively affects the energy balance. The purpose of the invention is to increase the efficiency of the process by improving the energy balance. The goal is achieved according to the method of continuous gasification of carbon-containing material in a reactor with molten iron by supplying carbon-containing material and oxygen-containing gas to the surface of the melt and evacuating those formed in the gas space above the surface of the gas melt in addition to the oxygen-containing gas jet supplied under the surface of the melt. on the surface of the melt from the height, at which the ratio of the distance between the spring opening of the feeding device oxygen and the melt surface to Diamé py means for supplying sour kind is 50-200. Technically pure oxygen is used as the gas jet supplied to the melt surface. Air is used as the gas jet supplied to the melt surface. The oxygen-containing gas stream supplied to the melt surface is preheated. An improved energy balance is achieved due to the fact that, when passing through the gas space above the melt surface, an oxygen-containing jet draws in gases that it burns and carries to the surface of the melt, so that the heat produced during the combustion of gases is transferred to the iron melt. In this case, the gas jet flows through the gas space above the surface of the bath as far as possible along a large path. Due to the radiation effect, the gas arising from the gasification of the fuel in the gas space is sucked in and captured. Since the gas stream directed to the surface of the melt contains oxygen, a part of the generated gases is burned. The resulting heat is transferred to the molten iron, because the gas jet directs the hot combustion products to the surface of the melt, so that the latter are in contact with the surface of the melt and can give off heat. Air is used as a gas stream, it is advisable to preheat it so that it does not divert: the heat necessary to heat the air from the gasification process. Preheating temperature is 300-400 ° C. Conventional pipelines and valves can be used for this temperature, in addition, it is economical to insulate supply systems. Technically pure oxygen can also be used as a gas jet, especially when using fuels with very low heat of combustion. The amount of oxygen in the gas jet is determined mainly by the economy and quality of the fuel used. Carbon-containing materials are fed to the iron melt under the surface of the melt. Carrier gases such as air, nitrogen, carbon monoxide, inert gas or the like are used for transportation. Oxygen purged through the gas space and above the surface of the gas jet melt is used to burn a portion of the gases produced from the fuel. The oxygen of the gasification process is fed through nozzles located below the surface of the melt, consisting of low concentric tubes, npirr M using hydrocarbons to protect the nozzles. In industrial installations, tubes with a diameter of 2050 mm are used. The amount of oxygen melted under the surface in relation to the amount of acids of the genus supplied in the gas stream above the melt surface varies widely; for example, 80% of the total amount of oxygen can be supplied in the gas jet from above, and only 20% below the melt surface or vice versa. About to at least 10% of the total amount of oxygen should be blown to the surface of the melt in the gas jet. In order to increase the efficiency of the process, the amount of oxygen supplied from above must be large, since it is supplied at a lower pressure than the pressure required to flow through the nozzles located beneath the surface of the melt. Preferably, several gas jets are directed onto the surface of the melt. The injection is carried out at a greater distance to the surface of the melt, approximately in the middle of the surface of the melt. The minimum distance between the gas jet nozzles and the melt surface is about 2 m. The nozzles are located in the refractory lining in the upper portion of the reactor. They can consist of a simple pipe with air injection or two concentric pipes using pure technical oxygen. In this case, the oxygen flows through the central tube, and to protect the nozzles in the annular gap, nitrogen, carbon monoxide, inert gas, hydrocarbon, or the like (0.15% in terms of oxidizing gas) is supplied in small quantities. A molten iron reactor produces a sulfur-free gas for combustion in boilers and heating systems, for example, to generate electricity from sulfur-containing fuels. In this case, sulfur is taken up in a reactor with molten iron-containing Slag Slag. These slag formers, in particular, CaO, are preferably supplied as a powder to oxygen-containing gases that are fed to the melt under its surface. The core formers are added to the fuel or CaO is blown together with the carrier gas.The resulting slag can be removed from the reactor in batches or to improve the heat balance, conduct desulfurization in the liquid state and introduce it into the reactor in the liquid state. Example 1. In a converter-type reactor, 70 tons of molten iron are contained. At the bottom of the reactor 10 nozzles with a diameter in the light of 24 mm are installed. Three nozzles are blown with coal containing,%: carbon 73, hydrogen 4, oxygen 13, water 1.5, sulfur 0.5 and ash 8, having a calorific value of 6,740 kcal / kg, Coal is blown in an amount of 350 kg / min, together with 18 nm / min of nitrogen. For the remaining nozzles, 200 nm / min of oxygen is simultaneously blown through. 66 nm / min of oxygen is blown into the surface of the melt from a height of 3 m by means of a water-cooled tube, the clear diameter of the annular outlet of which is 40 mm. Thus, oxygen is blown from a height at which the ratio of the distance between the outlet of the tube and the surface of the melt to the diameter of the tube is 75. At the same time, the degree of carbon monoxide burning to carbon dioxide is reached 20%. When half of the hydrogen contained in the coal is burned, additional heat of about 1.6 kcal / ton of coal is obtained, which is sufficient to melt about 1 ton of iron ore and bring it to 1520 C. Example 2. The process is carried out analogously to example 1, but oxygen is blown to the surface the melt from a height of 5 m, which corresponds to the ratio of the distance between the outlet of the water-cooled tube and the surface of the melt to the diameter of the tube equal to 125. In this case, the degree of burning out is 22%. The resulting additional heat is approximately 1.75 kcal / ton of coal. Example 3. The process is carried out similarly to npimepy 1, but oxygen is blown onto the surface of the melt from a height of 2 m, which corresponds to the J ratio of the distance between the outlet of the water-cooled tube and the surface of the melt to a tube diameter of 50. This burnout ratio is 14%, and additional heat of about 1.2 kcal / t coal. Example 4. Analogous to Example 1, but oxygen is blown from a height of 8 m, which corresponds to the ratio of the distance between the outlet of the tube and the surface of the melt To the diameter of the tube equal to 200. The degree of burnout is 12.5% and the additional heat is about 1 kcal. / t ang. Example 5. Analogous to example 3, but KIS. LOW is blown onto the surface of the melt from a height of 2 m using a tube with a light diameter of the exit orifice of 30 mm. Thus, the ratio of the distance between the outlet of the water-cooled tube and the surface of the melt is 66.6. The degree of burnout is 13.5%, and the additional heat is about t, 1 kcal / ton of coal. Example 6 (for comparison). The process is conducted as in Example 1, but oxygen is blown onto the surface 66 of the melt from a height of 1.5 m, which corresponds to the distance between the outlet of the water-cooled tube and the surface of the melt to a tube diameter of 37.5. The degree of burnout is 4.5%, and the additional heat is about 0.36 kcal / ton of coal. An example (for comparison). Similar to Example 1, but oxygen is blown onto the surface of the melt from a height of 1 m, which corresponds to the ratio of the distance between the outlet hole of the extruded tube and the surface of the melt to the diameter of the tube equal to 25. In this case, the degree of burning is 3.5%, and the additional heat is about O, 28 kcal / tonne coal. Example B (for comparison). The process is carried out analogously to Example 1, but oxygen is blown onto the surface of the melt from a height of 8.5 m, which corresponds to the ratio of the distance to the melad by the outlet of the water-cooled tube and the surface of the melt to the diameter of the tube equal to 212.5. The degree of burnout is 6%, and the additional heat is about 0.49 kcal / ton of coal.
    权利要求:
    Claims (4)
    [1]
    1. METHOD FOR CONTINUOUS GASIFICATION OF CARBON-CONTAINING MATERIAL IN THE REACTOR WITH THE MELTED IRON by supplying carbon-containing material and oxygen-containing gas to the surface of the melt and removing the gases formed in the gas space above the surface of the melt, which is characterized by the fact that by improving the energy balance, in addition to the gas supplied to the melt under its surface, an oxygen-containing gas stream is supplied to the melt surface from a height at which ix distance between the outlet of means for feeding kisloroda.i melt surface to the diameter of devices for supplying oxygen is 50-200.
    [2]
    2. The method according to claim 1, with the fact that technically pure oxygen is used as a gas stream supplied to the melt surface.
    [3]
    3. The method according to claim 1, characterized in that air is used as the gas jet supplied to the melt surface.
    [4]
    4. The method according to PP. 1-3, characterized in that the oxygen-containing gas stream supplied to the melt surface is subjected to preliminary heating.
    1 1148566
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    同族专利:
    公开号 | 公开日
    ES8206615A1|1982-08-16|
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    JPS5774390A|1982-05-10|
    HU188685B|1986-05-28|
    LU83573A1|1981-12-01|
    MX157845A|1988-12-16|
    ZA815676B|1982-08-25|
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    ATA333581A|1987-07-15|
    AU539665B2|1984-10-11|
    BE890047A|1981-12-16|
    PL130522B1|1984-08-31|
    DE3031680C2|1988-02-25|
    SE8104704L|1982-02-23|
    NL8103451A|1982-03-16|
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    CS253561B2|1987-11-12|
    ES504653A0|1982-08-16|
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    GB2082624A|1982-03-10|
    JPH01246311A|1989-10-02|
    FR2488903A1|1982-02-26|
    JPS6247473B2|1987-10-08|
    CA1181238A|1985-01-22|
    IT8123284D0|1981-07-31|
    GB2082624B|1984-03-14|
    BR8105352A|1982-05-18|
    JPH0762162B2|1995-07-05|
    AT385053B|1988-02-10|
    AU7440981A|1982-02-25|
    DE3031680A1|1982-03-11|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3031680A|DE3031680C2|1980-08-22|1980-08-22|
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